US8372365B2 - High pressure reduction-oxidation desulfurization process - Google Patents

High pressure reduction-oxidation desulfurization process Download PDF

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Publication number
US8372365B2
US8372365B2 US12/913,448 US91344810A US8372365B2 US 8372365 B2 US8372365 B2 US 8372365B2 US 91344810 A US91344810 A US 91344810A US 8372365 B2 US8372365 B2 US 8372365B2
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oxidizer
pressure
stream
absorber
gas
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US12/913,448
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US20120107205A1 (en
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Gary J. Nagl
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Merichem Technologies LLC
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Merichem Co
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Priority to US12/913,448 priority Critical patent/US8372365B2/en
Assigned to MERICHEM COMPANY reassignment MERICHEM COMPANY ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: NAGL, GARY J.
Priority to RU2013104511/05A priority patent/RU2527991C1/ru
Priority to PCT/US2011/050898 priority patent/WO2012057925A1/en
Priority to CN201510018697.XA priority patent/CN104667712B/zh
Priority to EP11761195.4A priority patent/EP2632569B1/en
Priority to BR112013003959A priority patent/BR112013003959B1/pt
Priority to JP2013536623A priority patent/JP5829692B2/ja
Priority to CN201180042300.0A priority patent/CN103079675B/zh
Priority to PL11761195T priority patent/PL2632569T3/pl
Priority to TW100135791A priority patent/TWI428169B/zh
Priority to TW103100079A priority patent/TWI477315B/zh
Publication of US20120107205A1 publication Critical patent/US20120107205A1/en
Priority to US13/736,314 priority patent/US8652435B2/en
Publication of US8372365B2 publication Critical patent/US8372365B2/en
Application granted granted Critical
Priority to RU2013136973/05A priority patent/RU2532558C1/ru
Priority to HK15107823.1A priority patent/HK1207027A1/xx
Priority to HK13111129.6A priority patent/HK1183837A1/xx
Assigned to MERICHEM TECHNOLOGIES, LLC reassignment MERICHEM TECHNOLOGIES, LLC ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: MERICHEM COMPANY
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8603—Removing sulfur compounds
    • B01D53/8612—Hydrogen sulfide
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/10—Oxidants
    • B01D2251/102—Oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/30—Alkali metal compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/90—Chelants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/90—Chelants
    • B01D2251/902—EDTA
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/90—Chelants
    • B01D2251/904—NTA
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/20—Metals or compounds thereof
    • B01D2255/207—Transition metals
    • B01D2255/20738—Iron
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/24—Hydrocarbons
    • B01D2256/245—Methane
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1468—Removing hydrogen sulfide

Definitions

  • This invention relates to an improved reduction-oxidization (Redox) process for treatment of sour gas streams containing hydrogen sulfide.
  • a high-pressure oxidizer is used in combination with a high-pressure absorber.
  • Hydrogen sulfide is a major source of pollution of gas streams since it is liberated as a waste by-product in a number of chemical processes, such as sulfate or kraft paper pulp manufacture, viscose manufacture, sewage treatment, the production of organic sulfur compounds, as well as during petroleum refining and in the production of natural gas and combustible gases from coal, such as in coking operations. Hydrogen sulfide is also present in geothermal steam, which is captured for use in power generating plants.
  • redox oxidation-reduction
  • a hydrogen sulfide-containing gas known as “sour gas”
  • a chelated metal catalyst to effect absorption.
  • the catalyst solution is then regenerated for reuse by contacting it with an oxygen-containing gas to oxidize the metal back to a higher oxidation state.
  • the elemental sulfur is continuously removed from the process as a solid product with high purity.
  • oxygen In order to return the “spent” liquid redox catalyst solution to its original oxidation level so it can be recycled for subsequent use in the process, oxygen must be supplied to the spent redox catalyst solution. This is typically accomplished using an oxidation process where various mechanical apparatus, including well-known tank spargers, use compressed air as the source of oxygen. Typically, such oxidation processes are operated at pressures lower than the pressure of the reduction portion of the process, i.e., the absorber, more typically at about atmospheric pressure. Use of low pressure oxidizers are a result of an attempt to minimize capital costs by eliminating the need for more expensive high pressure equipment. Although initial capital cost of equipment may be lower, operating at a large pressure differential between the absorber and the oxidizer has a host of other inherent problems.
  • the higher pressure redox solution exiting the absorber must be reduced in pressure before entering the oxidizer. This is typically accomplished through a flash drum or a series of flash drums. Reducing pressure of the redox solution has unfortunate consequences, such as foaming, lost of gas product, and rapid erosion of control valves due to the suspended solid sulfur particles. All of these problems reduce the overall process economics and the operability of the process.
  • This invention relates to an improved reduction oxidization process for use in treating hydrogen sulfide containing gas streams.
  • the improved process operates the oxidizer section of the process at a higher operating pressure than the reduction section, i.e., the absorber.
  • This higher pressure differential eliminates the need for pressure reducing equipment, such as a flash drum.
  • the design of the oxidizer is not critical to our process, likewise the design of the absorber is not critical, provided that both unit operations can operate at internal pressures greater than 100 psig and temperatures of approximately 125° F.
  • any oxygen containing gas can be used in this invention, the most commonly known and most available, air, will be referred to below for the sake of brevity.
  • Pressurized air introduced to the interior of the oxidizer maintains the operating pressure higher than the operating pressure of the absorber, which operates at pressures greater than 100 psig.
  • the oxidizer is controlled to operate at pressures about 5 to about 10 psi higher than the operating pressure of the absorber to minimize compression costs.
  • the higher pressure in the oxidizer is preferably maintained using high pressure air as the oxidizing gas to regenerate the metal catalyst solution, as explained below. Operating the oxidizer at pressures exceeding atmospheric results in a higher oxygen partial pressure within the oxidizer, and since the amount of oxygen required to reoxidize the catalyst is inversely proportional to the oxygen partial pressure less air is required as the oxidizer pressure is increased.
  • the high pressure absorber and oxidizer combination of my invention is preferably used in processes to treat hydrocarbon gas streams to convert H 2 S to elemental sulfur utilizing an aqueous redox solution containing a chelated iron catalyst.
  • the H 2 S containing gas stream (sour gas) is contacted with the aqueous redox solution where the H 2 S is absorbed and converted to elemental sulfur and where a portion of the iron is reduced from the ferric state (Fe +++ ) to the ferrous state (Fe ++ ). All or a portion of the redox solution containing the ferrous state iron is then introduced into an oxidizer where compressed air is introduced to the redox solution where it preferably contacts the redox solution as very tiny bubbles having a high surface area.
  • a preferred polyvalent metal is iron.
  • L represents the particular ligand chosen to formulate the metal chelate catalyst: H 2 S (gas) +H 2 O (liq.) ⁇ H 2 S (aqueous) +H 2 O (liq.) (1) H 2 S (aqueous) ⁇ H + +HS ⁇ (2) HS ⁇ +2(Fe 3+ L 2 ) ⁇ S (solid) +2(Fe 2+ L 2 )+H + (3)
  • the resulting equation is: H 2 S (gas) +2(Fe 3+ L 2 ) ⁇ 2H + +2(Fe 2+ L 2 )+S (solid) (4)
  • iron chelating agents capable of forming a complex in aqueous solutions with iron in the ferric valence state (Fe 3+ ) or in the ferrous valence state (Fe 2+ ) are suitable for use over the broad range of operating conditions employed for this oxidation-reduction system for the removal of hydrogen sulfide.
  • iron chelate reagents which have been used in prior art processes for removing hydrogen sulfide are the aminopolycarboxylic acid-type chelating agents, such as ethylenediamine tetraacetic acid and the alkali metal salts thereof.
  • one object of this invention is to eliminate the problems associated with a conventional redox process, such as foaming and loss of product gas in the flash drum(s) where the absorber is operated at high pressure and the oxidizer is operated at roughly atmospheric pressure.
  • any product gas which is dissolved in the solution leaving the high pressure absorber, will remain in solution until it reenters the high pressure absorber where a small amount of product gas will flash out of solution and enter the product gas stream.
  • the above-stated object is accomplished by providing an oxidizer that operates at a higher pressure than the absorber, preferably from about 5 to about 10 psi higher in pressure than the absorber.
  • the absorber preferably is operated at greater than 100 psig.
  • Another embodiment of our invention involves providing a system for oxidizing a liquid reduction-oxidation catalyst solution comprising a source of pressurized air; an oxidizer vessel capable of maintaining an operating pressure of P 2 , where P 2 ⁇ P 1 +5 psi and P 1 is the pressure of the absorber and is greater than 100 psig.
  • the pressurized air is fed to the oxidizer to regenerate the metal catalyst solution and to maintain the pressure differential between the absorber and the oxidizer.
  • Yet another embodiment of our invention relates to a process for continuously removing hydrogen sulfide from a gas where the gas feed is directed to the oxidation-reduction process where it is contacted with a chelated metal catalyst in an absorber operating at a pressure greater than 100 psig to produce a first stream of hydrogen sulfide-free product gas and a second stream comprising elemental sulfur and chelated metal catalyst solution; removing the first stream from the process; providing a high pressure oxidizer vessel operating at a pressure greater than the absorber; directing at least a portion of the second stream to the oxidizer along with a pressurized air stream to contact the second stream; and separating elemental sulfur from the chelated metal catalyst solution.
  • FIG. 1 schematically illustrates one possible embodiment of the redox process of my invention.
  • our invention concerns a novel high pressure oxidizer that can be used to regenerate a liquid redox catalyst solution.
  • This oxidizer can be used to provide a new process flow scheme for the desulphurization of a sour gas.
  • Operating temperatures for the oxidizer can range from about 25° C. to about 55° C.
  • Operating pressures are preferably greater than 100 psig and more preferably greater than 5 psi higher that the absorber operating pressure from which the oxidizer is in fluid communication.
  • FIGURE schematically illustrates such a desulfurization process 10 for treatment of gas streams contaminated with H 2 S.
  • a waste gas stream (sour gas) is delivered via feed line 1 to an absorber 2 where it is contacted with an aqueous chelated iron catalyst solution.
  • Absorber 2 is operated at a pressure greater than 100 psig.
  • the catalyst solution is obtained from high pressure oxidizer 3 via fluid control valve 4 .
  • the spent liquid catalyst solution is removed via line 5 and supplied via pump 6 through liquid level control valve 7 to the inlet of oxidizer 3 operating at a pressure 5 to 10 psi higher than the pressure in absorber 2 .
  • the absorber 2 may be of any suitable design to meet the required amount of H 2 S removal, i.e. liquid full absorbers, static mixers, packed columns, venturis or mobile bed absorbers.
  • the oxidized liquid redox solution is removed from oxidizer 3 through line 11 and introduced into absorber 2 .
  • the elemental sulfur is continuously removed from the process by sending a portion of the liquid solution from oxidizer 3 via stream 12 , to a lock hopper sulfur recovery device (not shown).
  • the oxidizer 3 pressure is maintained by the combination of high pressure air injection and the differential pressure controller 14 monitoring the absorber pressure and operating pressure control valve 15 on vent line 13 .
  • the invention thus far has been described with particular emphasis on the use of iron as the polyvalent metal of choice; however, other polyvalent metals that form chelates with the ligands described above can also be used.
  • additional polyvalent metals include copper, cobalt, vanadium, manganese, platinum, tungsten, nickel, mercury, tin and lead.
  • the chelating agents are generally of the aminopolycarboxylic acid family such as EDTA, HEDTA, MGDA and NTA, or others any one of which can be used in connection with this invention.
  • alkaline material In all liquid oxidation-reduction systems, some form of alkaline material must be added to the system to control the pH of the solution. Without the addition of the alkaline material, the pH of the solution will slowly decrease until absorption of H 2 S into the solution is no longer great enough to meet the required H 2 S removal efficiencies. This decrease in pH is due to the acidic nature of H 2 S. In addition, if the gas stream being processed contains other acidic species such as carbon dioxide, the pH will decrease even more quickly than with just H 2 S. Consequently, alkaline materials such as NaOH, KOH, ammonia, alkali metal carbonates, or bicarbonates are generally added to the system to neutralize the acidic components. These materials are generally added to the bulk solution contained in the oxidizer; however, they can be added anywhere in the process.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Analytical Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Water Supply & Treatment (AREA)
  • Gas Separation By Absorption (AREA)
  • Treating Waste Gases (AREA)
  • Catalysts (AREA)
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US12/913,448 2010-10-27 2010-10-27 High pressure reduction-oxidation desulfurization process Active 2031-08-12 US8372365B2 (en)

Priority Applications (15)

Application Number Priority Date Filing Date Title
US12/913,448 US8372365B2 (en) 2010-10-27 2010-10-27 High pressure reduction-oxidation desulfurization process
PL11761195T PL2632569T3 (pl) 2010-10-27 2011-09-08 Sposób na odsiarczanie pod wysokim ciśnieniem z reakcją redukcji/oksydacji
PCT/US2011/050898 WO2012057925A1 (en) 2010-10-27 2011-09-08 High pressure reduction-oxidation desulfurization process
CN201510018697.XA CN104667712B (zh) 2010-10-27 2011-09-08 高压氧化还原脱硫工艺
EP11761195.4A EP2632569B1 (en) 2010-10-27 2011-09-08 High pressure reduction-oxidation desulfurization process
BR112013003959A BR112013003959B1 (pt) 2010-10-27 2011-09-08 processo de dessulfurização por redução-oxidação em pressão elevada
JP2013536623A JP5829692B2 (ja) 2010-10-27 2011-09-08 高圧酸化還元脱硫法
CN201180042300.0A CN103079675B (zh) 2010-10-27 2011-09-08 高压氧化还原脱硫工艺
RU2013104511/05A RU2527991C1 (ru) 2010-10-27 2011-09-08 Способ непрерывного удаления сернистого водорода из потока газа
TW103100079A TWI477315B (zh) 2010-10-27 2011-10-03 高壓氧化還原脫硫方法
TW100135791A TWI428169B (zh) 2010-10-27 2011-10-03 高壓氧化還原脫硫方法
US13/736,314 US8652435B2 (en) 2010-10-27 2013-01-08 High pressure reduction-oxidation desulfurization process
RU2013136973/05A RU2532558C1 (ru) 2010-10-27 2013-08-07 Способ очистки от серы
HK15107823.1A HK1207027A1 (en) 2010-10-27 2013-09-29 High pressure reduction-oxidation desulfurization process
HK13111129.6A HK1183837A1 (en) 2010-10-27 2013-09-29 High pressure reduction-oxidation desulfurization process

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EP (1) EP2632569B1 (pt)
JP (1) JP5829692B2 (pt)
CN (2) CN103079675B (pt)
BR (1) BR112013003959B1 (pt)
HK (2) HK1183837A1 (pt)
PL (1) PL2632569T3 (pt)
RU (2) RU2527991C1 (pt)
TW (2) TWI428169B (pt)
WO (1) WO2012057925A1 (pt)

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CN103182237A (zh) * 2012-11-26 2013-07-03 广东依科电力技术有限公司 一种烟气脱硫系统
US9657248B1 (en) * 2014-03-14 2017-05-23 Biosystems Consulting, Inc. Systems, devices, compositions, and/or methods for de-sulphurizing acid gases
US9504984B2 (en) 2014-04-09 2016-11-29 Exxonmobil Upstream Research Company Generating elemental sulfur
FR3051459B1 (fr) 2016-05-20 2021-03-19 Centre Nat Rech Scient Installation et procede de traitement d'un flux comprenant du sulfure d'hydrogene
EA201990898A1 (ru) * 2016-10-14 2019-10-31 Обработка сероводорода в аэробных условиях
WO2018166937A1 (de) * 2017-03-14 2018-09-20 Siemens Aktiengesellschaft Verfahren und vorrichtung zur aufbereitung eines schwefelwasserstoffhaltigen gasstromes
CN106861401B (zh) * 2017-03-22 2020-04-07 武汉国力通能源环保股份有限公司 液化石油气脱硫净化系统及净化方法
CN108686486B (zh) * 2017-04-12 2021-01-15 北京华石联合能源科技发展有限公司 一种可再生的悬浮床湿法脱硫工艺
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CN108179044A (zh) * 2017-11-22 2018-06-19 中石化石油工程技术服务有限公司 基于湿式氧化还原法的带压再生脱硫系统
US10661220B2 (en) * 2018-02-27 2020-05-26 Merichem Company Hydrogen sulfide removal process
CN108970380B (zh) * 2018-09-07 2023-07-21 宜宾丝丽雅股份有限公司 一种以连续氧化除去废气中硫化氢的方法及装置
CN111514727A (zh) * 2020-04-13 2020-08-11 江苏亿超环境科技有限公司 一种用于车间酸性尾气排放的回收装置及方法
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US20130123561A1 (en) 2013-05-16
JP5829692B2 (ja) 2015-12-09
RU2532558C1 (ru) 2014-11-10
JP2014506180A (ja) 2014-03-13
US20120107205A1 (en) 2012-05-03
RU2527991C1 (ru) 2014-09-10
EP2632569A1 (en) 2013-09-04
PL2632569T3 (pl) 2017-08-31
TW201223622A (en) 2012-06-16
WO2012057925A1 (en) 2012-05-03
CN104667712B (zh) 2017-04-12
HK1207027A1 (en) 2016-01-22
CN104667712A (zh) 2015-06-03
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